Cu-CHA/Fe-MFI Mixed Zeolite Catalyst And Process For The Treatment Of NOx In Gas Streams

ABSTRACT

Described is a catalyst, preferably for use in selective catalytic reduction (SCR), said catalyst comprising one or more zeolites of the MFI structure type, and one or more zeolites of the CHA structure type, wherein at least part of the one or more zeolites of the MFI structure type contain iron (Fe), and wherein at least part of the one or more zeolites of the CHA structure type contain copper (Cu). An exhaust gas treatment system is described, comprising said catalyst as well as a process for the treatment of a gas stream comprising NO x  using said catalyst as well.

CROSS-REFERENCE TO RELATED APPLICATIONS

This application claims the benefit of priority under 35 U.S.C. §119(e)to U.S. Patent Application No. 61/321,907, filed Apr. 8, 2010, which ishereby incorporated by reference in its entirety.

TECHNICAL FIELD

The present invention relates to a catalyst which is preferably for usein selective catalytic reduction (SCR), as well as to an exhaust gastreatment system comprising said catalyst, and to a process for thetreatment of a gas stream comprising NO_(x). In particular, the presentinvention is concerned with a method of catalyzing the reduction ofnitrogen oxides, and especially with the selective reduction of nitrogenoxides with ammonia in the presence of oxygen, using metal-promotedzeolite catalysts.

BACKGROUND

The emissions present in the exhaust gas of a motor vehicle can bedivided into two groups. Thus, the term “primary emission” refers topollutant gases which form directly through the combustion process ofthe fuel in the engine and are already present in the untreated emissionbefore it passes through an exhaust gas treatment system. Secondaryemission refers to those pollutant gases which can form as by-productsin the exhaust gas treatment system.

The exhaust gas of lean engines comprises, as well as the customaryprimary emissions of carbon monoxide CO, hydrocarbons HC and nitrogenoxides NO_(x), a relatively high oxygen content of up to 15% by volume.In the case of diesel engines, there is additional particulate emissionin addition to the gaseous primary emissions, which consistspredominantly of soot residues, with or without organic agglomerates,and originates from partially incomplete fuel combustion in thecylinder.

In diesel engine applications, the use of specific diesel particulatefilters is unavoidable for the removal of the particulate emissions.Furthermore, complying with the emissions limits prescribed bylegislation in Europe and the United States requires nitrogen oxideremoval from the exhaust gas (“denitrification”). Thus, although carbonmonoxide and hydrocarbon pollutant gases from the lean exhaust gas caneasily be rendered harmless by oxidation over a suitable oxidationcatalyst, the reduction of the nitrogen oxides to nitrogen is much moredifficult owing to the high oxygen content of the exhaust gas stream.

Known methods for removing nitrogen oxides from exhaust gases arefirstly methods using nitrogen oxide storage catalysts (NSCs) andsecondly methods for selective catalytic reduction (SCR) by means ofammonia over a suitable catalyst, SCR catalyst for short.

The cleaning action of nitrogen oxide storage catalysts is based on thenitrogen oxides being stored in a lean operating phase of the engine bythe storage material of the storage catalyst, predominantly in the formof nitrates. When the storage capacity of the NSC is exhausted, thecatalyst has to be regenerated in a subsequent rich operating phase ofthe engine. This means that the nitrates formed beforehand aredecomposed and the nitrogen oxides released again are reacted with thereducing exhaust gas components over the storage catalyst to givenitrogen, carbon dioxide and water.

Since the implementation of a rich operating phase in diesel engines isnot straightforward and the establishment of the rich exhaust gasconditions required for regeneration of the NSC frequently entailsauxiliary measures such as fuel postinjection into the exhaust gas line,the alternative SCR method is preferably used for denitrification ofdiesel motor vehicle exhaust gases. In this method, according to theengine design and construction of the exhaust gas system, a distinctionis made between “active” and “passive” SCR methods, “passive” SCRmethods involving use of ammonia secondary emissions generateddeliberately in the exhaust gas system as a reducing agent fordenitrification.

For example, U.S. Pat. No. 6,345,496 B1 describes a method for cleaningengine exhaust gases, in which repeatedly alternating lean and richair/fuel mixtures are established and the exhaust gas thus produced ispassed through an exhaust gas system which comprises, on the inflowside, a catalyst which converts NO_(x) to NH₃ only under rich exhaustgas conditions, while a further catalyst arranged on the outflow sideadsorbs or stores NO_(x) in the lean exhaust gas, and releases it underrich conditions, such that it can react with NH₃ generated by theinflow-side catalyst to give nitrogen. As an alternative, according toU.S. Pat. No. 6,345,496 B1, an NH₃ adsorption and oxidation catalyst maybe arranged on the outflow side, which stores NH₃ under rich conditions,desorbs it under lean conditions and oxidizes it with oxygen to givenitrogen and water. Further disclosures of such methods are known. Likethe use of the nitrogen oxide storage catalysts, however, such “passive”SCR methods have the disadvantage that one of their essentialconstituents is the provision of rich exhaust gas conditions, which aregenerally required for in situ generation of ammonia as a reducingagent.

Compared to this, in “active” SCR methods, the reducing agent is meteredinto the exhaust gas line from an addition tank carried in the vehicleby means of an injection nozzle. Such a reducing agent used may, apartfrom ammonia, also be a compound readily decomposable to ammonia, forexample urea or ammonium carbamate. Ammonia has to be supplied to theexhaust gas at least in a stoichiometric ratio relative to the nitrogenoxides. Owing to the greatly varying operation conditions of the motorvehicles, the exact metered addition of the ammonia is notstraightforward. This leads in some cases to considerable ammoniabreakthroughs downstream of the SCR catalyst. To prevent secondaryammonia emission, an oxidation catalyst is usually arranged downstreamof the SCR catalyst, which is intended to oxidize ammonia which breaksthrough to nitrogen. Such a catalyst is referred to hereinafter as anammonia slip catalyst.

To remove particulate emissions from the exhaust gas of diesel motorvehicles, specific diesel particulate filters are used, which may beprovided with an oxidation catalyst-containing coating to improve theirproperties. Such a coating serves to lower the activation energy foroxygen-based particulate burnoff (soot combustion) and hence to lowerthe soot ignition temperature on the filter, to improve the passiveregeneration performance by oxidation of nitrogen monoxide present inthe exhaust gas to nitrogen dioxide, and to suppress breakthroughs ofhydrocarbon and carbon monoxide emissions.

If compliance with legal emissions standards requires bothdenitrification and removal of particulates from the exhaust gas ofdiesel motor vehicles, the described measures for removing individualpollutant gases are combined in a corresponding conventional exhaust gassystem by connection in series. For example, WO 99/39809 describes anexhaust after treatment system wherein an oxidation catalyst foroxidation of NO in NO_(x) to NO₂, a particulate filter, a metering unitfor a reducing agent and an SCR catalyst follow on each other. Toprevent ammonia breakthroughs, an additional ammonia slip catalyst isgenerally required downstream of the SCR catalyst, and continues theseries of catalysts on the outflow side of the SCR catalyst.

In this respect, both synthetic and natural zeolites and their use inpromoting certain reactions, including the selective reduction ofnitrogen oxides with ammonia in the presence of oxygen, are well knownin the art. Zeolites are aluminosilicate crystalline materials havingrather uniform pore sizes which, depending upon the type of zeolite andthe type and amount of cations included in the zeolite lattice, mayrange from about 3 to 10 angstroms in diameter.

EP 1 961 933 A1, for example, relates to a diesel particulate filter fortreating exhaust gas comprising a filter body having provided thereon anoxidation catalyst coating, an SCR-active coating, and an ammoniastorage material. Among the materials which may be used as thecatalytically active component in the SCR reaction, said documentmentions the use of zeolites selected from beta zeolite, Y-zeolite,faujasite, mordenite and ZSM-5 which may be exchanged with iron orcopper.

EP 1 147 801 A1, on the other hand, relates to a process for reducingnitrogen oxides present in a lean exhaust gas from an internalcombustion engine by SCR using ammonia, wherein the reduction catalystpreferably contains ZSM-5 zeolite exchanged with copper or iron. Saiddocument further concerns an SCR catalyst having a honeycomb substrateand deposited thereon a coating containing ZSM-5 zeolite exchanged withiron.

EP 2 123 614 A2 for its part concerns a honeycomb structure containingzeolites and an inorganic binder. In particular, a first zeoliteincluded in said structure is ion-exchange with a metal including Cu,Mn, Ag, and V, and a second zeolite is further included which isexchanged with a metal including Fe, Ti, and Co. Regarding the types ofzeolites used for the first and second zeolite, these include zeolitebeta, zeolite Y, ferrierite, ZSM-5 zeolite, mordenite, faujasite,zeolite A, and zeolite L.

U.S. Pat. No. 7,332,148 B2 describes a stabilized aluminosilicatezeolite containing copper or iron, wherein the stabilized zeoliteincludes ZSM-5, ZSM-8, ZSM-11, ZSM-12, zeolite X, zeolite Y, zeolitebeta, mordenite, and erionite.

Finally, WO 2008/106519 A1 describes a zeolite having the CHA crystalstructure and containing copper. Said document also discusses the use ofsuch an ion-exchanged zeolite as an SCR catalyst.

Accordingly, the prior art relates an awareness of the utility ofmetal-promoted zeolite catalysts including, among others, iron-promotedand copper-promoted zeolite catalysts, in particular for the selectivecatalytic reduction of nitrogen oxides with ammonia.

Presently, however, increasingly strict legislature with respect toemissions, and in particular regarding motor vehicle exhaust gasemissions, requires improved catalysts and exhaust treatment systemsusing such catalysts for the treatment thereof. Thus, exhaust gasemission legislation in the European Union for exhaust gas emissionstage Euro 6 now requires reduction of NO_(x) emissions for mostpassenger cars powered by diesel engines. For this purpose, exhaust gasemissions are tested using the New European Driving Cycle (NEDC), alsoreferred to as the MVEG (Motor Vehicle Emissions Group) cycle, which islaid down in European Union Directive 70/220/EEC. One way of meetingthis requirement includes the application of SCR catalyst technology tothe exhaust gas systems of the vehicles in question.

As opposed to the old European driving cycle (ECE-15) driving cycle, aparticular feature of the NEDC is that it integrates a so-calledextra-urban driving cycle, such that testing may better represent thetypical usage of a car in Europe, and, accordingly, the typical emissionpattern linked thereto. More specifically, in the NEDC, the old Europeandriving cycle ECE-15 is performed in the time period of 0 to 800seconds, after which the extra-urban driving cycle is conducted in thetime period up to 1200 seconds.

It would be desirable to provide an improved catalyst, in particular foruse in selective catalytic reduction, wherein said catalyst is, forexample, better adapted to the actual emission conditions encountered inmotor vehicle use, such as for example those encountered in the NEDC.

SUMMARY

The present invention includes the following embodiments, wherein theseinclude the specific combinations of embodiments as indicated by therespective interdependencies defined therein:

-   1. A catalyst, preferably for use in selective catalytic reduction    (SCR), said catalyst comprising    -   one or more zeolites of the MFI structure type, and    -   one or more zeolites of the CHA structure type,    -   wherein at least part of the one or more zeolites of the MFI        structure type contain iron (Fe), and wherein at least part of        the one or more zeolites of the CHA structure type contain        copper (Cu).-   2. The catalyst of embodiment 1, wherein the weight ratio of the one    or more zeolites of the MFI structure type relative to the one or    more zeolites of the CHA structure type ranges from 1:10 to 10:1,    preferably from 1:5 to 5:1, more preferably form 1:2 to 2:1, more    preferably from 0.7:1 to 1:0.7, more preferably from 0.8:1 to 1:0.8,    and even more preferably from 0.9:1 to 1:0.9.-   3. The catalyst of embodiment 1 or 2, wherein one or more of the    zeolites, and preferably all of the zeolites, comprise both Al and    Si in their respective zeolite frameworks.-   4. The catalyst of embodiment 3, wherein the molar ratio of silica    to alumina (SAR) in the one or more zeolites of the MFI structure    type ranges from 5 to 150, preferably from 15 to 100, more    preferably from 20 to 50, more preferably from 23 to 30, and even    more preferably from 25 to 27.-   5. The catalyst of embodiment 3 or 4, wherein the molar ratio of    silica to alumina (SAR) in the one or more zeolites of the CHA    structure type ranges from 5 to 100, preferably from 10 to 70, more    preferably from 20 to 55, more preferably from 25 to 35, and even    more preferably from 28 to 32.-   6. The catalyst of any of embodiments 1 to 5, wherein the amount of    Fe in the one or more zeolites of the MFI structure type ranges from    0.1 to 15 wt.-% based on the weight of said one or more zeolites,    wherein preferably the amount of Fe ranges from 0.5 to 10 wt.-%,    more preferably from 1.0 to 7.0 wt.-%, more preferably from 2.5 to    5.5 wt.-%, more preferably from 3.5 to 4.2 wt.-%, and even more    preferably from 3.7 to 4.0 wt.-%.-   7. The catalyst of any of embodiments 1 to 6, wherein the amount of    Cu in the one or more zeolites of the CHA structure type ranges from    0.05 to 15 wt.-% based on the weight of said one or more zeolites,    wherein preferably the amount of Cu ranges from 0.1 to 10 wt.-%,    more preferably from 0.5 to 5.0 wt.-%, more preferably from 1.0 to    4.0 wt.-%, more preferably from 1.6 to 3.4 wt.-%, and even more    preferably from 1.8 to 3.2 wt.-%.-   8. The catalyst of any of embodiments 1 to 7, wherein said catalyst    further comprises a substrate, preferably a honeycomb substrate,    onto which the one or more zeolites are provided.-   9. The catalyst of embodiment 8 wherein the substrate is selected    from the group consisting of flow-through substrates and wall-flow    substrates, preferably from the group consisting of cordierite    flow-through substrates and wall-flow substrates, and silicon    carbide flow-through substrates and wall-flow substrates.-   10. The catalyst of embodiment 8 or 9, wherein the catalyst    comprises one or more layers, preferably washcoat layers, provided    on the substrate, the zeolites being contained in one single layer    or two or more separate layers, wherein preferably the zeolites are    contained in one single layer.-   11. The catalyst of any of embodiments 1 to 10, wherein either the    one or more zeolites of the MFI structure type, or the one or more    zeolites of the CHA structure type, or both the one or more zeolites    of the MFI structure type and the one or more zeolites of the CHA    structure type, are respectively present in the catalyst in a    loading ranging from 0.1 to 5.0 g/in³, preferably from 0.7 to 2.0    g/in³, more preferably from 1.0 to 1.7 g/in³, more preferably from    1.15 to 1.55 g/in³, more preferably from 1.25 to 1.45 g/in³, more    preferably from 1.32 to 1.38 g/in³, and even more preferably from    1.34 to 1.36 g/in³.-   12. The catalyst of any of embodiments 1 to 11, comprised in an    exhaust gas treatment system comprising an internal combustion    engine and an exhaust gas conduit in fluid communication with the    internal combustion engine, wherein said catalyst is present in the    exhaust gas conduit, and wherein the internal combustion engine is    preferably a lean burn engine, and more preferably a diesel engine.-   13. An exhaust gas treatment system comprising an internal    combustion engine and an exhaust gas conduit in fluid communication    with the internal combustion engine, wherein a catalyst according to    any of embodiments 1 to 11 is present in the exhaust gas conduit,    and wherein the internal combustion engine is preferably a lean burn    engine, and more preferably a diesel engine.-   14. The exhaust gas treatment system of embodiment 13, said exhaust    gas treatment system further comprising an oxidation catalyst and/or    a catalyzed soot filter (CSF), wherein the oxidation catalyst and/or    the CSF are preferably located upstream from the catalyst according    to any of embodiments 1 to 11, and wherein the oxidation catalyst is    a diesel oxidation catalyst (DOC) in instances where the internal    combustion engine is a diesel engine.-   15. A process for the treatment of a gas stream comprising NO_(x)    comprising conducting said gas stream over and/or through a catalyst    according to any one of embodiments 1 to 11, wherein the gas stream    is preferably an exhaust gas stream, more preferably an exhaust gas    stream resulting from an internal combustion engine, and even more    preferably a diesel exhaust gas stream.-   16. The process for the treatment of a gas stream comprising NO_(x)    according to embodiment 15, wherein the gas stream comprises ammonia    and/or urea.-   17. The process for the treatment of a gas stream comprising NO_(x)    according to embodiment 15 or 16, wherein prior to the contacting of    the catalyst with the gas stream, the NO₂ content thereof is 80    wt.-% or less based on 100 wt.-% of NO_(x), wherein preferably the    NO₂ content is comprised in the range of from 5 to 70 wt.-%, more    preferably of from 10 to 60 wt.-%, more preferably of from 15 to 55    wt.-%, and even more preferably of from 20 to 50 wt.-%.

BRIEF DESCRIPTION OF THE DRAWINGS

FIG. 1 is a graph displaying results from NEDC testing of the catalystcompositions according to Example 1 and Comparative Examples 2 and 3,respectively, wherein the testing period in seconds is plotted on thex-axis, and the NO_(x) emissions in grams NO_(x) is plotted on they-axis, and wherein the background displays the legally prescribedcourse of NEDC testing over the time period in terms of the variation ofthe motor vehicle's speed as laid down in the European Union Directive70/220/EEC.

FIG. 2 is a graph displaying the total NO_(x) conversion in % achievedfor samples according to Example 1 and Comparative Examples 2 and 3,respectively, in NEDC testing.

DESCRIPTION

In this respect, it has surprisingly been found that according to thepresent invention as outlined in the following, an improved catalyst maybe provided. In particular, it has unexpectedly been found that acatalyst comprising zeolites of both the MFI and of the CHA structuretype, wherein the MFI-type zeolites contain iron and the CHA-typezeolites contain copper, display clearly improved catalytic properties,in particular when used in SCR applications.

Thus, the present invention relates to a catalyst, preferably for use inselective catalytic reduction (SCR), said catalyst comprising

one or more zeolites of the MFI structure type, and

one or more zeolites of the CHA structure type,

wherein at least part of the one or more zeolites of the MFI structuretype contain iron (Fe), and

wherein at least part of the one or more zeolites of the CHA structuretype contain copper (Cu).

Within the meaning of the present invention, the term “selectivecatalytic reduction” abbreviated as “SCR” refers to any catalyticprocess involving the reaction of nitrogen oxides NO_(x) with areductant. In particular, SCR refers to reduction reactions, whereinNO_(x) is transformed to a reduction product thereof, which ispreferably N₂. Regarding the term “reductant”, said term refers to anysuitable reducing agent for the SCR process, wherein preferably ammoniaand/or any ammonia precursor such as urea and/or ammonium carbamate ispreferred, urea being preferably comprised in the ammonia precursor.Even more preferably, the term “reductant” refers to ammonia. The term“reductant” may, however, further include hydrocarbons and/orhydrocarbon derivatives such as oxygenated hydrocarbons, such as forexample those which may be found in motor vehicle fuels and/or in motorvehicle exhaust gas, in particular in diesel fuel and/or diesel exhaustgas.

According to embodiments of the present invention, any conceivablezeolite of the MFI or of the CHA structure type may be used,respectively, provided that it displays the typical structuralcharacteristics of that structure-type. With respect to the one or morezeolites of the MFI structure, these may for example comprise one ormore zeolites selected from the group consisting of ZSM-5,[As—Si—O]-MFI, [Fe—Si—O]-MFI, [Ga—Si—O]-MFI, AMS-1B, AZ-1, Bor-C,Boralite C, Encilite, FZ-1, LZ-105, Monoclinic H-ZSM-5, Mutinaite, NU-4,NU-5, Silicalite, TS-1, TSZ, TSZ-III, TZ-01, USC-4, USI-108, ZBH,ZKQ-1B, ZMQ-TB, organic-free ZSM-5, and mixtures of two or more thereof.According to preferred embodiments of the present invention, the one ormore zeolites of the MFI structure type include ZSM-5.

Concerning the one or more zeolites of the CHA structure, these maycomprise one or more zeolites selected from the group consisting ofchabazite, AlP, [Al—As—O]-CHA, [Co—Al—P—O]-CHA, [Mg—Al—P—O]-CHA,[Si—O]-CHA, [Zn—Al—P—O]-CHA, [Zn—As—O]-CHA, |Co|[Be—P—O]-CHA,|Li—Na|[Al—Si—O]-CHAO-34, CoAPO-44, CoAPO-47, DAF-5, DehydratedNa-Chabazite, GaPO-34, K-Chabazite, LZ-218, Linde D, Linde R, MeAPO-47,MeAPSO-47, Ni(deta)₂-UT-6, Phi, SAPO-34, SAPO-47, SSZ-13, SSZ-62,UiO-21, Willhendersonite, ZK-14, ZYT-6, and mixtures of two or morethereof. According to preferred embodiments of the present invention,the one or more zeolites of the CHA structure type comprise one or morezeolites selected from the group consisting of chabazite, SSZ-13,LZ-218, Linde D, Linde R, Phi, ZK-14, and ZYT-6, and mixtures of two ormore thereof, wherein more preferably, the one or more zeolites of theCHA structure type include chabazite.

According to embodiments of the present invention which are furtherpreferred, the one or more zeolites of the MFI structure type includeZSM-5 and the one or more zeolites of the CHA structure type compriseone or more zeolites selected from the group consisting of chabazite,SSZ-13, LZ-218, Linde D, Linde R, Phi, ZK-14, and ZYT-6, and mixtures oftwo or more thereof, wherein even more preferably, the one or morezeolites of the MFI structure type include ZSM-5 and the one or morezeolites of the CHA structure type include chabazite. According toparticularly preferred embodiments, the one or more zeolites of the MFIstructure type is ZSM-5 and the one or more zeolites of the CHAstructure type is chabazite

According to an embodiment of the present invention, at least part ofthe one or more MFI-type zeolites contain iron and at least part of theone or more CHA-type zeolites contain copper.

With respect to the iron contained in at least part of the one or moreMFI-type zeolites and the copper contained in at least part of the oneor more CHA-type zeolites, said metals may respectively be containedtherein in any conceivable fashion and in any conceivable state. Thus,according to the present invention, there is no particular limitationwith respect to the oxidation state of iron and copper contained in thecatalyst, nor with respect to the way in which they are contained in therespective type of zeolite. Preferably, however, iron and/or copper, andmore preferably both iron and copper, respectively display a positivestate of oxidation in the respective zeolite. Furthermore, iron and/orcopper may be contained on the zeolite surface and/or within the porousstructure of the respective zeolite framework. Alternatively or inaddition to being supported on the zeolite surface and/or within theporous structure thereof, iron and/or copper may be included in thezeolite framework, for example by isomorphous substitution. According topreferred embodiments, the iron and/or copper, and more preferably bothiron and copper, are supported on the respective zeolite surface and/orwithin the porous structure thereof, and even more preferably both onthe respective zeolite surface and within the porous structure thereof.According to particularly preferred embodiments of the presentinvention, both iron and copper are respectively contained in at leastpart of the one or more zeolites of the MFI and CHA structure type in apositive oxidation state, wherein said iron and copper is supported onthe surface of the respective zeolite, including being contained withinthe porous structure thereof.

The catalyst according to an embodiment of the present invention maycomprise the one or more zeolites of the MFI structure type and the oneor more zeolites of the CHA structure type in any conceivable weightratio, wherein it is preferred that the weight ratio of the one or morezeolites of the MFI structure type relative to the one or more zeolitesof the CHA structure type ranges from 1:10 to 10:1, more preferably from1:5 to 5:1, more preferably form 1:2 to 2:1, more preferably from 0.7:1to 1:0.7, more preferably from 0.8:1 to 1:0.8, and even more preferablyfrom 0.9:1 to 1:0.9.

According to particularly preferred embodiments of the presentinvention, the weight ratio of the MFI-type zeolites to the CHA-typezeolites is approximately 1:1.

According to an embodiment of the present invention, it is preferredthat the one or more zeolites of the MFI structure type and/or the oneor more zeolites of the CHA structure type respectively comprise both Aland Si in their frameworks, wherein it is more preferred that both thezeolites of the MFI structure type and the zeolites of the CHA structuretype respectively comprise both Al and Si in their frameworks. Thus,according to an embodiment of the present invention, it is preferredthat one or more of the zeolites, and more preferably all of thezeolites, comprise both Al and Si in their respective zeoliteframeworks.

With respect to embodiments of the present invention wherein one or moreof the zeolites comprise both Al and Si in their respective frameworks,said zeolites may in principle display any possible ratio of Al to Si.In embodiments of the present invention wherein one or more zeolites ofthe MFI structure type comprise both Al and Si in their framework, it ishowever preferred that the molar ratio of silica to alumina (SAR) in theone or more zeolites of the MFI structure type ranges from 5 to 150,more preferably from 15 to 100, more preferably from 20 to 50, morepreferably from 23 to 30, and even more preferably from 25 to 27.Furthermore, in embodiments of the present invention wherein one or morezeolites of the CHA structure type comprise both Al and Si in theirframework, it is preferred that the SAR in the one or more zeolites ofthe CHA structure type ranges from 5 to 100, preferably from 10 to 70,more preferably from 20 to 55, more preferably from 25 to 35, and evenmore preferably from 28 to 32. According to particularly preferredembodiments of the present invention wherein one or more zeolites ofboth the MFI and the CHA structure type respectively comprise Al and Siin their framework, it is further preferred that the SAR in the one ormore MFI-type zeolites ranges from 5 to 150, and the one or moreCHA-type zeolites ranges from 5 to 100, more preferably that the SAR inthe one or more MFI-type zeolites ranges from 15 to 100, and the one ormore CHA-type zeolites ranges from 10 to 70, more preferably that theSAR in the one or more MFI-type zeolites ranges from 20 to 50, and theone or more CHA-type zeolites ranges from 20 to 55, more preferably thatthe SAR in the one or more MFI-type zeolites ranges from 23 to 30, andthe one or more CHA-type zeolites ranges from 25 to 35, and even morepreferably that the SAR in the one or more MFI-type zeolites ranges from25 to 27, and the one or more CHA-type zeolites ranges from 28 to 32.

Regarding the iron contained in the MFI-type zeolites and the amount ofcopper contained in the CHA-type zeolites, there is no particularlimitation according to the present invention as to their respectiveamounts. It is, however, preferred according to the present invention,that the amount of iron (Fe) in the one or more zeolites of the MFIstructure type is comprised in the range of from 0.1 to 15 wt.-% basedon the weight of said one or more zeolites of the MFI structure type,wherein more preferably the amount of Fe ranges from 0.5 to 10 wt.-%,more preferably from 1.0 to 7.0 wt.-%, more preferably from 2.5 to 5.5wt.-%, more preferably from 3.5 to 4.2 wt.-%, and even more preferablyfrom 3.7 to 4.0 wt.-%. Furthermore, it is preferred according to thepresent invention that the amount of copper (Cu) in the one or morezeolites of the CHA structure type ranges from 0.05 to 15 wt.-% based onthe weight of said one or more zeolites of the CHA structure type,wherein more preferably the amount of Cu ranges from 0.1 to 10 wt.-%,more preferably from 0.5 to 5.0 wt.-%, more preferably from 1.0 to 4.0wt.-%, more preferably from 1.6 to 3.4 wt.-%, and even more preferablyfrom 1.8 to 3.2 wt.-%. According to particularly preferred embodimentsof the present invention, the amount of iron in the one or more MFI-typezeolites ranges from 0.1 to 15 wt.-%, and the amount of copper in theone or more CHA-type zeolites ranges from 0.1 to 10 wt.-%, wherein morepreferably the amount of iron in the one or more MFI-type zeolitesranges from 1.0 to 7.0 wt.-%, and the amount of copper in the one ormore CHA-type zeolites ranges from 0.5 to 5.0 wt.-%, more preferably theamount of iron in the one or more MFI-type zeolites ranges from 2.5 to5.5 wt.-%, and the amount of copper in the one or more CHA-type zeolitesranges from 1.0 to 4.0 wt.-%, more preferably the amount of iron in theone or more MFI-type zeolites ranges from 3.5 to 4.2 wt.-%, and theamount of copper in the one or more CHA-type zeolites ranges from 1.6 to3.4 wt.-%, and even more preferably, the amount of iron in the one ormore MFI-type zeolites ranges from 3.7 to 4.0 wt.-%, and the amount ofcopper in the one or more CHA-type zeolites ranges from 1.8 to 3.2wt.-%.

According to the present invention, the catalyst may be provided in anyconceivable form, such as by way of example in the form of a powder, agranulate, or a monolith. In this respect, it is particularly preferredthat the catalyst further comprises a substrate, onto which the one ormore zeolites are provided. In general, the substrate can be made frommaterials commonly known in the art. For this purpose, porous materialsare preferably used as the substrate material, in particular ceramic andceramic-like materials such as cordierite, α-alumina, analuminosilicate, cordierite-alumina, silicon carbide, aluminum titanate,silicon nitride, zirconia, mullite, zircon, zircon mullite, zirconsilicate, sillimanite, a magnesium silicate, petalite, spodumene,alumina-silica-magnesia and zirconium silicate, as well as porousrefractory metals and oxides thereof. According to the presentinvention, “refractory metal” refers to one or more metals selected fromthe group consisting of Ti, Zr, Hf, V, Nb, Ta, Cr, Mo, W, and Re. Thesubstrate may also be formed of ceramic fiber composite materials.According to the present invention, the substrate is preferably formedfrom cordierite, silicon carbide, and/or from aluminum titanate, andeven more preferably from cordierite and/or silicon carbide.

The substrates useful for the catalysts of embodiments of the presentinvention may also be metallic in nature and be composed of one or moremetals or metal alloys. The metallic substrates may be employed invarious shapes such as corrugated sheet or monolithic form. Suitablemetallic supports include the heat resistant metals and metal alloyssuch as titanium and stainless steel as well as other alloys in whichiron is a substantial or major component. Such alloys may contain one ormore of nickel, chromium and/or aluminum, and the total amount of thesemetals may advantageously comprise at least 15 wt.-% of the alloy, e.g.,10-25 wt.-% of chromium, 3-8 wt.-% of aluminum and up to 20 wt.-% ofnickel. The alloys may also contain small or trace amounts of one ormore other metals such as manganese, copper, vanadium, titanium and thelike. The surface or the metal substrates may be oxidized at hightemperatures, e.g., 1000° C. and higher, to improve the resistance tocorrosion of the alloys by forming an oxide layer on the surfaces thesubstrates.

Furthermore, the substrate according to the present invention may be ofany conceivable shape, provided that it allows for the fluid contactwith at least a portion of the respective one or more zeolites of theMFI and CHA structure types present thereon. Preferably, the substrateis a monolith, wherein more preferably the monolith is a flow-throughmonolith. Suitable substrates include any of those materials typicallyused for preparing catalysts, and will usually comprise a ceramic ormetal honeycomb structure. Accordingly, the monolithic substratecontains fine, parallel gas flow passages extending from an inlet to anoutlet face of the substrate, such that passages are open to fluid flow(referred to as honeycomb flow through substrates). The passages, whichare essentially straight paths from their fluid inlet to their fluidoutlet, are defined by walls onto which the one or more zeolites of theMFI and CHA structure types are respectively disposed, so that the gasesflowing through the passages may contact them. The flow passages of themonolithic substrate are thin-walled channels, which can be of anysuitable cross-sectional shape and size such as trapezoidal,rectangular, square, sinusoidal, hexagonal, oval, or circular. Suchstructures may contain up to 900 gas inlet openings (i.e., cells) persquare inch of cross section, wherein according to the present inventionstructures preferably have from 50 to 600 openings per square inch, morepreferably from 300 to 500, and even more preferably from 350 to 400.

Thus, according to a preferred embodiment of the present invention, thecatalyst comprises a substrate which is a monolith, and preferably ahoneycomb substrate.

According to further preferred embodiments of the present invention, thesubstrate is a wall flow monolith. For these embodiments, the substrateis preferably a honeycomb wall flow filter, wound or packed fiberfilter, open-cell foam, or sintered metal filter, wherein wall flowfilters are particularly preferred. As for the equally preferred flowthrough monoliths, useful wall flow substrates have a plurality of fine,substantially parallel gas flow passages extending along thelongitudinal axis of the substrate. Typically, each passage is blockedat one end of the substrate body, with alternate passages blocked atopposite end-faces. Particularly preferred wall flow substrates for usein the present invention include thin porous walled honeycomb monoliths,through which a fluid stream may pass without causing too great anincrease in back pressure or pressure across the catalyst. Ceramic wallflow substrates used in the present invention are preferably formed of amaterial having a porosity of at least 40%, preferably from 40 to 70%,and having a mean pore size of at least 5 microns, preferably from 5 to30 microns. Further preferred are substrates having a porosity of atleast 50% and having a mean pore size of at least 10 microns.

Thus, according to the present invention, the substrate preferablycomprised in the catalyst is preferably selected from the groupconsisting of flow-through substrates and wall-flow substrates, morepreferably from the group consisting of cordierite flow-throughsubstrates and wall-flow substrates, and silicon carbide flow-throughsubstrates and wall-flow substrates.

In general, according to embodiments of the present invention whichfurther comprise a substrate, the zeolites may be provided thereon inany conceivable fashion, wherein they are preferably provided thereon inthe form of one or more layers which are preferably washcoat layers. Inpreferred embodiments of the present invention, wherein the catalystcomprises a substrate and two or more layers provided thereon, thezeolites may be provided in said two or more layers in any possiblemanner. Accordingly, the present invention includes, for example, suchpreferred embodiments wherein the zeolites are contained in only asingle of the two or more layers, as well as embodiments wherein thezeolite is contained in more than one of the two or more layers.Preferably, however, the zeolites are contained in a single layer,irrespective of the number of layers present on the substrate.

Thus, according to preferred embodiments of the present inventionwherein the catalyst comprises a substrate, it is further preferred thatthe catalyst comprises one or more layers, preferably washcoat layers,provided on the substrate, the zeolites being contained in one singlelayer or two or more separate layers, wherein preferably the zeolitesare contained in one single layer.

In further embodiments of the present invention comprising a substrateand two or more layers provided thereon, wherein the zeolites arecontained in more than one of said layers, there is no particularlimitation as to the distribution of the one or more zeolites of the MFIand the CHA structure type among said more than one layers whichcomprise said zeolites. Thus, it is principally possible according tothe present invention, that, for example, the MFI- and CHA-type zeolitesare respectively contained in each of the layers which contain zeolites,or that, alternatively, only part of the layers containing zeolitescontain both MFI- and CHA-type zeolites. Furthermore, it is possibleaccording to said further embodiments of the present invention that nosingle layer contains both MFI- and CHA-type zeolites, said zeolitesbeing accordingly contained in separate layers of the catalyst.According to the present invention it is, however, preferred that atleast one of the layers in such embodiments contains both MFI- andCHA-type zeolites, wherein it is even more preferred that each of thetwo or more layers of said embodiments containing the zeolites alsocontains both the MFI- and CHA-type zeolites.

In principle, the one or more zeolites of the MFI and of the CHAstructure type may be respectively present in the catalyst in anyconceivable amount, provided that an improved catalyst according to thepresent invention may be obtained. Thus, either the one or more zeolitesof the MFI structure type, or the one or more zeolites of the CHAstructure type, or both the one or more zeolites of the MFI structuretype and the one or more zeolites of the CHA structure type, mayrespectively be present in the catalyst in a loading ranging from 0.1 to5.0 g/in³, wherein their loading preferably ranges from 0.7 to 2.0g/in³, more preferably from 1.0 to 1.7 g/in³, more preferably from 1.15to 1.55 g/in³, more preferably from 1.25 to 1.45 g/in³, more preferablyfrom 1.32 to 1.38 g/in³, and even more preferably from 1.34 to 1.36g/in³. In particular, the respective loadings of the MFI- and CHA-typezeolites may be independent from one another, in the sense that thepreferred loading ranges may apply either to the MFI- or to the CHA-typezeolites, wherein the loading of the one or more zeolites belonging tothe other structure type is respectively not particularly limited, andmay therefore be present in any loading, or may be limited to adifferent range of loadings. Thus, the present invention also comprisesembodiments wherein, for example, the loading of the MFI-type zeolitesranges from 0.1 to 5.0 g/in³, and the loading of the CHA-type zeolitesranges from 1.34 to 1.36 g/in³, or embodiments wherein, for example, theloading of the MFI-type zeolites ranges from 0.7 to 2.0 g/in³, and theloading of the CHA-type zeolites ranges from 1.32 to 1.38 g/in³, orembodiments wherein, for example, the loading of the MFI-type zeolitesranges from 1.0 to 1.7 g/in³, and the loading of the CHA-type zeolitesranges from 1.25 to 1.45 g/in³, or embodiments wherein, for example, theloading of the MFI-type zeolites ranges from 1.15 to 1.55 g/in³, and theloading of the CHA-type zeolites ranges from 1.15 to 1.55 g/in³, orembodiments wherein, for example, the loading of the MFI-type zeolitesranges from 1.25 to 1.45 g/in³, and the loading of the CHA-type zeolitesranges from 1.0 to 1.7 g/in³, or embodiments wherein, for example, theloading of the MFI-type zeolites ranges from 1.32 to 1.38 g/in³, and theloading of the CHA-type zeolites ranges from 0.7 to 2.0 g/in³, orembodiments wherein, for example, the loading of the MFI-type zeolitesranges from 1.34 to 1.36 g/in³, and the loading of the CHA-type zeolitesranges from 0.1 to 5.0 g/in³.

In addition to the above-mentioned catalyst, the present invention alsorelates to a treatment system for an exhaust gas stream. In particular,the treatment system of the present invention comprises an internalcombustion engine which is preferably a lean burn engine, and even morepreferably a diesel engine. According to the present invention, it ishowever also possible to use a lean burn gasoline engine in saidtreatment system.

Furthermore, the treatment system according to an embodiment of thepresent invention comprises an exhaust gas conduit which is in fluidcommunication with the internal combustion engine. In this respect, anyconceivable conduit may be used, provided that it is capable ofconducting exhaust gas from an internal combustion engine, and maysufficiently resist the temperatures and the chemical speciesencountered in the exhaust gas of an internal combustion engine, inparticular of a lean burn engine such as a diesel engine. Within themeaning of the present invention, the fluid communication providedbetween the exhaust gas conduit and the internal combustion enginesignifies that the treatment system allows for the constant passage ofexhaust gas from the engine to the conduit.

According to the exhaust gas treatment system of an embodiment of thepresent invention, the catalyst is present in the exhaust gas conduit.In general, the catalyst may be provided in the exhaust gas conduit inany conceivable fashion, provided that it is present within the exhaustgas conduit in the sense that it may be contacted by the exhaust gaspassing through said conduit. Preferably, the catalyst is provided inthe exhaust gas conduit on a substrate as outlined in the presentapplication, and in particular on a honeycomb substrate, which ispreferably either a flow-through or a wall-flow honeycomb substrate.

Thus, an embodiment of the present invention also relates to an exhaustgas treatment system comprising an internal combustion engine and anexhaust gas conduit in fluid communication with the internal combustionengine, wherein the catalyst according to the present invention ispresent in the exhaust gas conduit, and wherein the internal combustionengine is preferably a lean burn engine, and more preferably a dieselengine.

In this respect and independently thereof, the present invention alsorelates to embodiments wherein the inventive catalyst is comprised in anexhaust gas treatment system comprising an internal combustion engineand an exhaust gas conduit in fluid communication with the internalcombustion engine, wherein said catalyst is present in the exhaust gasconduit, and wherein the internal combustion engine is preferably a leanburn engine, and more preferably a diesel engine.

According to preferred embodiments of the present invention, the exhaustgas treatment system further comprises a means of introducing areductant into the exhaust gas stream, wherein said means is locatedupstream from the inventive MFI/CHA-zeolite catalyst. In particular, itis preferred that a means of introducing ammonia and/or urea into theexhaust gas conduit is provided. In this respect, any means known to theskilled person may be provided, in particular those commonly applied toexhaust gas treatment systems operating with active SCR methodsnecessitating the direct introduction of said reductants. According toparticularly preferred embodiments, the reductant which preferablycomprises ammonia and/or urea is introduced by the means of an injectionnozzle provided in the exhaust gas conduit upstream from the inventivecatalyst.

Within the meaning of the present invention, the exhaust gas treatmentsystem may suitably further comprise any further components for theeffective treatment of an exhaust gas. In particular, said systempreferably further comprises an oxidation catalyst or a catalyzed sootfilter (CSF) or both an oxidation catalyst and a CSF. According to saidembodiments, the oxidation catalyst and/or the CSF are also presentwithin the exhaust gas conduit.

In the present invention, any suitable CSF can be used, provided that itmay effectively oxidize soot which may be contained in the exhaust gas.To this effect, the CSF of the present invention preferably comprises asubstrate coated with a washcoat layer containing one or more catalystsfor burning off trapped soot and/or oxidizing exhaust gas streamemissions. In general, the soot burning catalyst can be any knowncatalyst for combustion of soot. For example, the CSF can be coated witha one or more high surface area refractory oxides (such as e.g. alumina,silica, silica alumina, zirconia, and zirconia alumina) and/or with anoxidation catalyst (such as e.g. a ceria-zirconia) for the combustion ofunburned hydrocarbons and to some degree particulate matter. However,preferably the soot burning catalyst is an oxidation catalyst comprisingone or more precious metal catalysts, said one or more precious metalcatalysts preferably comprising one or more metals selected from thegroup consisting of platinum, palladium, and rhodium.

Regarding the oxidation catalyst preferably comprised in the exhaust gastreatment system instead of or in addition to a CSF, any oxidationcatalyst may be used to this effect which is suitable for oxidizingunburned hydrocarbons, CO, and/or NO_(x) comprised in the exhaust gas.In particular, oxidation catalysts are preferred which comprise one ormore precious metal catalysts, and more preferably one or more preciousmetals selected from the group consisting of platinum, palladium, andrhodium. According to particularly preferred embodiments of the presentinvention, wherein the internal combustion engine of the exhaust gastreatment system is a diesel engine, the oxidation catalyst ispreferably a diesel oxidation catalyst. In particular, within themeaning of the present invention, a “diesel oxidation catalyst” refersto any oxidation catalyst which is particularly well adapted to theoxidation of diesel exhaust gas, in particular with respect to thetemperatures and to the composition of diesel exhaust gas encountered inthe treatment thereof.

According to particularly preferred embodiments, the exhaust gastreatment system further comprises a CSF, and even more preferably botha CSF and an oxidation catalyst. Even more preferably, the exhaust gastreatment system further comprises a CSF and a diesel oxidationcatalyst.

In principle, in embodiments of the exhaust gas treatment system whichfurther comprise an oxidation catalyst and/or a CSF, said furthercomponents may be present in the exhaust gas conduit in any order and atany emplacement therein, provided that the effective treatment of anexhaust gas may be provided. In particular, however, the presence and/ororder and/or location of said further components may depend on the type,on the state, in particular with respect to the temperature and pressurethereof, and on the average composition of the exhaust gas which istreated. Thus depending on the application of the exhaust gas treatmentsystem, the present invention includes preferred embodiments wherein theoxidation catalyst and/or the CSF are located upstream or downstreamfrom the inventive MFI/CHA-zeolite catalyst, as well as preferredembodiments comprising both an oxidation catalyst and a CSF, wherein theoxidation catalyst is located upstream and the CSF downstream thereof,or wherein, vice versa, the CSF is located upstream, and the oxidationcatalyst downstream thereof. According to particularly preferredembodiments of the present invention, the oxidation catalyst and/or theCSF are located upstream from the inventive MFI/CHA-zeolite catalyst,wherein even more preferably, the exhaust gas treatment system comprisesboth an oxidation catalyst and a CSF upstream from the inventiveMFI/CHA-zeolite catalyst. Within the meaning of the present invention,“upstream” and “downstream” relates to the direction of flow of theexhaust gas through the exhaust gas conduit in fluid communication withthe internal combustion engine.

Thus, an embodiment of the present invention also relates to an exhaustgas treatment system as defined in the foregoing, said exhaust gastreatment system further comprising an oxidation catalyst and/or acatalyzed soot filter (CSF), wherein the oxidation catalyst and/or theCSF are preferably located upstream from the inventive MFI/CHA-zeolitecatalyst, and wherein the oxidation catalyst is a diesel oxidationcatalyst (DOC) in instances where the internal combustion engine is adiesel engine.

Furthermore, as outlined in the foregoing, the exhaust gas treatmentsystem preferably further includes a means of introducing a reductantinto the exhaust gas conduit, said means being located upstream from theinventive MFI/CHA-zeolite catalyst. In particular, said means enablesthe introduction of a reductant comprising ammonia and/or urea into theexhaust gas conduit. Accordingly, the present invention also relates toan exhaust gas treatment system wherein in addition to or instead offurther comprising an oxidation catalyst and/or a catalyzed soot filter(CSF) respectively preferably located upstream from the inventiveMFI/CHA-zeolite catalyst, the oxidation catalyst being a dieseloxidation catalyst (DOC) in instances where the internal combustionengine is a diesel engine, said system further comprises a means ofintroducing a reductant preferably comprising ammonia and/or urea intothe exhaust gas conduit, said means being located upstream of theinventive MFI/CHA-zeolite catalyst.

According to further preferred embodiments of the present invention, theexhaust gas treatment system further comprises an ammonia slip catalystlocated downstream of the MFI/CHA-zeolite catalyst for oxidizing excessammonia and/or urea which has not reacted in the SCR. Regarding thepreferred ammonia slip catalyst, said catalyst may be provided in theexhaust gas conduit in any manner commonly known in the art, providedthat it may effectively oxidize said excess ammonia and/or urea. Inparticular, said preferred embodiments involve an exhaust gas treatmentsystems according to the present invention which include a means ofintroducing a reductant into the exhaust gas conduit as defined in theforegoing.

In addition to a catalyst and to an exhaust gas treatment systemcomprising said catalyst, the present invention further concerns aprocess for the treatment of a gas stream comprising NO_(x). In general,in the process of the present invention, any suitable gas streamcomprising NO_(x) may be employed, provided that its state andcomposition are both suited for being treated when contacted with aMFI/CHA-zeolite catalyst according to the present invention, whereinpreferably said treatment at least in part involves the selectivecatalytic reduction of at least part of the NO_(x) contained in saidgas. For this purpose, the gas stream used in the inventive processpreferably contains at least one reductant, which is preferably ammoniaand/or any ammonia precursor such as urea and/or ammonium carbamate,urea being preferably comprised in the ammonia precursor. According tofurther embodiments of the inventive process, however, the gas streamused may also contain hydrocarbons and/or hydrocarbon derivatives suchas oxygenated hydrocarbons, such as for example those which may be foundin motor vehicle fuels and/or in motor vehicle exhaust gas, inparticular in diesel fuel and/or exhaust gas. Said further reductantsmay be contained in the gas treated in the inventive process either inaddition to ammonia, or, according to further embodiments, may also becontained therein instead of ammonia. According to the presentinvention, it is however particularly preferred that the gas comprisesammonia and/or urea as a reducing agent for the treatment of exhaust gasemissions, in particular via SCR.

Thus, an embodiment of the present invention also relates to a processfor the treatment of a gas stream comprising NO_(x) as defined in thepresent application, wherein the gas stream comprises ammonia and/orurea.

Regarding the content of reductant in the gas stream, said reductantpreferably comprising ammonia and/or urea, there is no particularlimitation in this respect, provided that at least part of the NO_(x) insaid gas may be reduced by SCR when contacting the MFI/CHA-zeolitecatalyst of the present invention. It is however preferred, that saidcontent does not considerably derive from the amount of reductantnecessary for the maximal conversion of NO_(x) by the catalyst. In thisrespect, the maximal conversion reflects the maximum amount of NO_(x)which may be converted by SCR at a given time point in the inventiveprocess, i.e. relative to the actual state and condition of both thecatalyst and the gas to be treated upon contacting thereof, and inparticular depending on the content of the reductant and, preferably,depending on the amount of ammonia and/or urea contained therein.Accordingly, the maximal conversion of NO_(x) directly reflects themaximum amount of reductant, and preferably of ammonia and/or urea,which may react with NO_(x) in the SCR process at a given time point.

According to preferred embodiments of the present invention, the gasstream used in the inventive process is preferably an exhaust gas streamcomprising NO_(x). In this respect, there is no particular limitation asto the process which leads to such an exhaust gas stream, provided thatit is suited for treatment with the MFI/CHA-zeolite catalyst accordingto the present invention, or may be processed to a gas stream suited fortreatment with such a catalyst. According to the inventive process it isfurther preferred that the exhaust gas stream is an exhaust gas streamresulting from an internal combustion engine, and even more preferablyfrom a lean burn engine. According to particularly preferredembodiments, the exhaust gas stream is a diesel engine exhaust gasstream.

In the process according to an embodiment of the present invention, thegas stream is contacted with the inventive MFI/CHA-zeolite catalyst fortreatment thereof, wherein said contacting is achieved by eitherconducting the gas stream over the catalyst, or conducting the gasstream through the catalyst. Said contacting may, however, also beachieved by conducting the gas stream both over and through theinventive catalyst. According to preferred embodiments, the gas streamis either conducted over the catalyst, wherein the catalyst preferablycomprises a flow-through substrate for this purpose, or the gas streamis conducted through the catalyst, wherein in this case the catalystpreferably comprises a wall-flow substrate. When using a wall-flowsubstrate, however, there are instances wherein, depending on theprocess conditions and the specific form and dimensions of the catalyst,at least a portion of the gas stream may also be conducted over thecatalyst. According particularly preferred embodiments of the inventiveprocess, the catalyst used in the inventive process either comprises awall-flow honeycomb substrate or a flow-through honeycomb substrate.

Thus, an embodiment of the present invention also relates to a processfor the treatment of a gas stream comprising NO_(x) comprisingconducting said gas stream over and/or through an MFI/CHA-zeolitecatalyst according to the present invention, wherein the gas stream ispreferably an exhaust gas stream, more preferably an exhaust gas streamresulting from an internal combustion engine, and even more preferably adiesel exhaust gas stream.

In the inventive process, there is no particular limitation as to theamount of NO_(x) contained in the gas stream, wherein preferably, theamount thereof in the gas streams used in the inventive process does notexceed 10 wt.-% based on the total weight of the exhaust gas, and morepreferably does not exceed 1 wt.-%, more preferably 0.5 wt.-%, morepreferably 0.1 wt-%, more preferably 0.05 wt-. %, more preferably 0.03wt-. %, and even more preferably does not exceed 0.01 wt.-%.

Regarding the specific composition of the NO_(x) fraction contained inthe gas stream treated in the inventive process, there is no limitationas to the type or to the content of specific nitrous oxide gases NO_(x)contained therein. According to specific embodiments of the presentinvention, it is however preferred that the NO₂-content relative to thetotal NO_(x)-content is 80 wt.-% or less based on 100 wt.-% of NO_(x),wherein more preferably, the NO₂ content is comprised in the range offrom 5 to 70 wt.-%, more preferably of from 10 to 60 wt.-%, morepreferably of from 15 to 55 wt.-%, and even more preferably of from 20to 50 wt.-%.

In general, the composition of the gas stream used in the inventiveprocess as defined in the present application refers to the gas streamprior to its use in the inventive process, and in particular prior tothe contacting thereof with the catalyst. Preferably, however, saidcomposition refers to the gas stream's composition immediately prior tocontacting the catalyst, i.e. immediately before treatment thereofbegins by catalyzed chemical conversion thereof.

Thus, an embodiment of the present invention also relates to a processfor the treatment of a gas stream comprising NO_(x) as defined in thepresent application, wherein prior to the contacting of the catalystwith the gas stream, the NO₂ content thereof is 80 wt.-% or less basedon 100 wt.-% of NO_(x), wherein preferably the NO₂ content is comprisedin the range of from 5 to 70 wt.-%, more preferably of from 10 to 60wt.-%, more preferably of from 15 to 55 wt.-%, and even more preferablyof from 20 to 50 wt.-%.

The catalyst according to the present invention can be readily preparedby processes well known in the prior art. A representative process isset forth below. As used herein, the term “washcoat” has its usualmeaning in the art of a thin, adherent coating of a catalytic or othermaterial applied to a substrate carrier material, such as ahoneycomb-type carrier member, which is preferably sufficiently porousto permit the passage there through of the gas stream being treated.

The several zeolite components of the catalyst may be applied to thesubstrate as mixtures of one or more components in sequential steps in amanner which will be readily apparent to those skilled in the art ofcatalyst manufacture. A typical method of manufacturing the catalyst ofthe present invention is to respectively provide the at least onezeolite of the MFI structure type, and the at least one further zeoliteof the CHA structure type as a coating or washcoat layer on the walls ofa particularly preferred flow-through or wall-flow honeycomb substrate.According to certain preferred embodiments of the present invention, thezeolites are provided in a single washcoat on the substrate.

The catalyst according to the present invention is however preferablyprepared by further using at least one binder, wherein any conceivablebinder used in the art of catalyst manufacture, and in particular in theart of automotive SCR catalyst manufacture, may be used. In thisrespect, a silica-alumina binder is for example preferably used for thepreparation of the inventive catalyst, wherein said binder may beprovided together with one or more of the zeolite components, and ispreferably provided together with the zeolite components in one or morecoatings on a substrate, more preferably in one or more washcoat layers.

For preparing the inventive catalyst, the components of one or possiblymore washcoat layers may respectively be processed to a slurry,preferably to an aqueous slurry. The substrate may then be sequentiallyimmersed into the respective slurries for applying the individualwashcoats, after which excess slurry is removed to provide a thincoating of the two or more slurries on the walls of the substrate. Thecoated substrate is then dried and preferably calcined to provide anadherent coating of the respective component to the walls of thesubstrate. Thus, for example, after providing a first washcoat layer onthe substrate, and preferably drying and/or calcining the coatedsubstrate, the resulting coated substrate may then be immersed into afurther slurry to form a second washcoat layer deposited over the firstwashcoat layer. Again, the substrate may then be dried and/or calcinedand eventually coated with a third washcoat, which again maysubsequently be dried and/or calcined to provide a finished catalyst inaccordance with one embodiment of the present invention. Regarding thesteps of drying, washing, and calcining of the catalyst coated in thisfashion, these may be respectively performed in the manner well known inthe art of catalyst manufacture, in particular regarding the solventsand/or solutions used for washing the coated catalyst, as well asregarding the temperature, duration, and the atmosphere employed in thesteps of drying and calcination, respectively. Concerning the step ofcalcination, any possible temperature may be used therein, provided thatthe process leads to the desired transformations in the catalyst withoutcausing any notable or substantial deterioration of the catalystsstability, in particular with regard to its use in SCR. Thus, in certaincases, the temperature of calcination will not exceed 700° C.,preferably 650° C., more preferably 600° C., and even more preferablywill not exceed 550° C. Thus, calcination may for example be conductedat a temperature comprised in the range of from 500° C. to 650° C.,preferably 550° C. to 600° C., more preferably 570° C. to 590° C., morepreferably, and even more preferably at a temperature comprised in therange of from 575° C. to 585° C.

When preparing the inventive catalyst in the above-mentioned manner, itis however preferred that no washing of the washcoat layers is performedafter the application and optional drying thereof.

Accordingly, the catalyst of the present invention may be preparedaccording to a process comprising

(a) providing at least one zeolite of the MFI structure type, and atleast one further zeolite selected from zeolites of the CHA structuretype, wherein at least part of the one or more zeolites of the MFIstructure type contain iron, and wherein at least part of the one ormore further zeolites of the CHA structure type contain copper;(b) preparing one or more washcoat compositions respectively comprisingone or more of the zeolites;(c) applying the one or more washcoat compositions in one morerespective layers onto the substrate, wherein a step of drying isoptionally conducted after the respective application of one or more ofthe individual layers;(d) optionally washing and/or drying the coated substrate, wherein thecoated substrate is preferably not washed; and(e) optionally subjecting the coated substrate to a calcination process.

Embodiments of the present invention may be better understood by thefollowing non-limiting examples.

EXAMPLES Example 1

A catalyst composition was prepared comprising 1.35 g/in³ of a zeoliteof the CHA structure type, said CHA-type zeolite having a silica toalumina ratio (SAR) of approximately 30 and containing 3 wt.-% of copperbased on the total weight of the CHA-type zeolite, 1.35 g/in³ of azeolite of the MFI structure type, said MFI-type zeolite having a silicato alumina ratio of approximately 26 and containing 3.8 wt.-% of ironbased on the total weight of the MFI-type zeolite, and 0.3 g/in³ of asilica-alumina binder.

Comparative Example 2

A catalyst composition was prepared comprising 1.9 g/in³ of a zeolite ofthe CHA structure type, said CHA-type zeolite having a silica to aluminaratio (SAR) of approximately 30 and containing 3 wt.-% of copper basedon the total weight of the CHA-type zeolite, and 0.1 g/in³ of a zirconylbinder.

Comparative Example 3

A catalyst composition was prepared comprising 1.35 g/in³ of a zeoliteof the BEA structure type, said BEA-type zeolite having a silica toalumina ratio (SAR) of approximately 40 and containing 1.3 wt.-% of ironbased on the total weight of the BEA-type zeolite, 1.35 g/in³ of azeolite of the MFI structure type, said MFI-type zeolite having a silicato alumina ratio of approximately 26 and containing 3.8 wt.-% of ironbased on the total weight of the MFI-type zeolite, and 0.3 g/in³ of asilica-alumina binder.

SCR Performance Testing

DeNO_(x) Performance of the SCR Catalysts were evaluated in transientconditions using the New European Driving Cycle, also referred to as theMVEG (Motor Vehicle Emissions Group) cycle. In particular, testingconditions were such, that the NO_(x) fraction of the exhaust gas streamcontained less than 30 wt.-% of NO₂ based on the total NO_(x)-content.

For testing, the catalyst compositions according to Examples 1 andComparative Examples 2 and 3 were respectively coated onto a5.66″×5.66″×6″ flow-through honeycomb substrate having a volume of 2.5L, a cell density of 400 cells per square inch, and a wall thickness ofapproximately 100 μm (4 mil). The catalyst samples prepared in thisfashion were then tested in an exhaust gas treatment system with adiesel oxidation catalyst (DOC) and a catalyzed soot filter (CSF)respectively located upstream from the tested catalyst.

The results from the NEDC catalyst testing are shown in FIGS. 1 and 2,respectively. Thus, as may be taken from said figures, the inventivecatalyst according to Example 1 which contains a combination of CHA- andMFI-type zeolites displays a clearly improved performance compared tothe catalyst sample of Comparative Example 2 which only containsCHA-type zeolite. In particular, as may be taken from FIG. 2, theinventive catalyst leads to a considerably higher level of conversion ofthe NO_(x) emissions compared to the catalyst of Comparative Example 2.Furthermore, when considering the results displayed in FIG. 1, whereinthe level of NO_(x) emissions is plotted as a function of the NEDCtesting period, the inventive catalyst shows a superior conversionperformance compared to Comparative Example 2 both during the periodfrom 0 to 800s corresponding to the old European driving cycle (ECE-15),as well as during the testing period from 800 to 1200s, corresponding tothe extra-urban part of the driving cycle involving higher spacevelocity and higher NO_(x) mass flow.

Compared to testing results for Comparative Example 3 in FIG. 1, whichas opposed to the specific MFI/CHA-zeolite mixture of the inventiveexample contains a mixture of iron-exchanged zeolites or the MFI and BEAstructure types, the inventive catalyst shows a somewhat poorerperformance during the low temperature and moderate space velocityportion of the NEDC testing (cf. FIG. 1). Said initial performance is,however, well compensated by an outstanding conversion rate at higherspace velocities and higher NO_(x) mass flow. Thus, as may be taken fromthe overall performance results displayed in FIG. 2, the inventivecatalyst is also superior to a catalyst according to Comparative Example3. In particular, although the performance of a catalyst according toComparative Example 3 is somewhat better adapted to the representativeurban driving conditions encounter in the 0 to 800s time period of theNEDC, the inventive catalyst is clearly superior over the entire cycledue to the outstanding performance in the extra-urban cycle sectionbetween 800 and 1200s. Accordingly, when considering the overallcatalyst performance, the inventive catalyst is better adapted to theactual exhaust gas emission pattern of a vehicle over time, whenconsidering the actual driving behavior of the average passenger carreflected in NEDC testing.

Consequently, the catalyst according to the present invention shows aclearly superior performance in SCR compared to a catalyst according tothe prior art represent by Comparative Example 2, and, furthermore, isparticularly well adapted to the actual driving conditions encounteredin motor vehicle use, as reflected in NEDC testing. In particular, theseexcellent results may be attributed to the use of a specific combinationof zeolite materials as defined by the catalyst of the presentinvention.

1. A catalyst, preferably for use in selective catalytic reduction(SCR), said catalyst comprising one or more zeolites of the MFIstructure type, and one or more zeolites of the CHA structure type,wherein at least part of the one or more zeolites of the MFI structuretype contain iron (Fe), and wherein at least part of the one or morezeolites of the CHA structure type contain copper (Cu).
 2. The catalystof claim 1, wherein the weight ratio of the one or more zeolites of theMFI structure type relative to the one or more zeolites of the CHAstructure type ranges from 1:10 to 10:1.
 3. The catalyst of claim 1,wherein one or more of the zeolites comprise both Al and Si in theirrespective zeolite frameworks.
 4. The catalyst of claim 3, wherein themolar ratio of silica to alumina (SAR) in the one or more zeolites ofthe MFI structure type ranges from 5 to
 150. 5. The catalyst of claim 3,wherein the molar ratio of silica to alumina (SAR) in the one or morezeolites of the CHA structure type ranges from 5 to
 100. 6. The catalystof claim 1, wherein the amount of Fe in the one or more zeolites of theMFI structure type ranges from 0.1 to 15 wt.-% based on the weight ofsaid one or more zeolites.
 7. The catalyst of claim 1, wherein theamount of Cu in the one or more zeolites of the CHA structure typeranges from 0.05 to 15 wt.-% based on the weight of said one or morezeolites.
 8. The catalyst of claim 1, wherein said catalyst furthercomprises a honeycomb substrate onto which the one or more zeolites areprovided.
 9. The catalyst of claim 8, wherein the substrate is selectedfrom the group consisting of flow-through substrates and wall-flowsubstrates.
 10. The catalyst of claim 8, wherein the catalyst comprisesone or more washcoat layers provided on the substrate, the zeolitesbeing contained in one single layer.
 11. The catalyst of claim 1,wherein either the one or more zeolites of the MFI structure type, orthe one or more zeolites of the CHA structure type, or both the one ormore zeolites of the MFI structure type and the one or more zeolites ofthe CHA structure type, are respectively present in the catalyst in aloading ranging from 0.1 to 5.0 g/in³.
 12. An exhaust gas systemcomprising the catalyst of claim 1, an internal combustion engine and anexhaust gas conduit in fluid communication with the internal combustionengine, wherein said catalyst is present in the exhaust gas conduit, andwherein the internal combustion engine is a lean burn engine.
 13. Anexhaust gas treatment system comprising an internal combustion engineand an exhaust gas conduit in fluid communication with the internalcombustion engine, wherein a catalyst according to claim 1 is present inthe exhaust gas conduit, and wherein the internal combustion engine is adiesel engine.
 14. The exhaust gas treatment system of claim 13, saidexhaust gas treatment system further comprising an oxidation catalystand/or a catalyzed soot filter (CSF), wherein the oxidation catalystand/or the CSF are located upstream from the catalyst according to claim1, and wherein the oxidation catalyst is a diesel oxidation catalyst(DOC).
 15. A process for the treatment of a gas stream comprising NO_(x)comprising conducting said gas stream over a catalyst according to claim1, wherein the gas stream an exhaust gas stream a diesel exhaust gasstream.
 16. The process for the treatment of a gas stream comprisingNO_(x) according to claim 15, wherein the gas stream comprises ammoniaand/or urea.
 17. The process for the treatment of a gas streamcomprising NO_(x) according to claim 15, wherein prior to the contactingof the catalyst with the gas stream, the NO₂ content thereof is 80 wt.-%or less based on 100 wt.-% of NO_(x).
 18. The catalyst of claim 1,wherein the weight ratio of the one or more zeolites of the MFIstructure type relative to the one or more zeolites of the CHA structuretype ranges from 1:2 to 2:1.
 19. The catalyst of claim 3, wherein themolar ratio of silica to alumina (SAR) in the one or more zeolites ofthe MFI structure type ranges from 23 to
 30. 20. The catalyst of claim3, wherein the molar ratio of silica to alumina (SAR) in the one or morezeolites of the CHA structure type ranges from 25 to
 35. 21. Thecatalyst of claim 1, wherein the amount of Fe in the one or morezeolites of the MFI structure type ranges from 2.5 to 5.5 wt.-% based onthe weight of said one or more zeolites.
 22. The catalyst of claim 1,wherein the amount of Cu in the one or more zeolites of the CHAstructure type ranges from 1.6 to 3.4 wt.-% based on the weight of saidone or more zeolites.
 23. The catalyst of claim 1, wherein either theone or more zeolites of the MFI structure type, or the one or morezeolites of the CHA structure type, or both the one or more zeolites ofthe MFI structure type and the one or more zeolites of the CHA structuretype, are respectively present in the catalyst in a loading ranging from1.25 to 1.45 g/in³.